PROCESS FOR THE PRODUCTION OF 17-Oxabicyclo[14.1.0]heptadec-8-ene

ABSTRACT

The invention relates to a process for producing 17-oxabicyclo[14.1.0]heptadec-8-ene comprising a reaction with the reactants cyclohexadeca-1,9-diene and hydrogen peroxide.

FIELD OF THE INVENTION

The present invention relates to a process for producing 17-oxabicyclo[14.1.0]heptadec-8-ene from cyclohexadeca-1,9-diene (CHDD).

PRIOR ART

17-Oxabicyclo[14.1.0]heptadec-8-ene is an intermediate stage of the musk fragrance 8-cyclohexadecen-1-one and may be produced by already-known production processes. DE2111753 and DE112007000301 each disclose the production of 17-oxabicyclo[14.1.0]heptadec-8-ene from cyclohexadeca-1,9-diene using peroxy acids.

OBJECT OF THE INVENTION

It is the object of the present invention to selectively epoxidize cyclohexadeca-1,9-diene at a double bond to 17-oxabicyclo[14.1.0]heptadec-8-ene. The reaction must be capable of being carried out economically, with high yield, under sustainable conditions with high selectivity, minimal use of energy, minimal consumption of raw materials, few by-products, high reaction velocity, minimal system corrosion, and in an atom-efficient and environmentally friendly manner. In particular, the formation of undesired diepoxides is to be avoided or minimized because, among other things, these can be difficult to separate from the desired monoepoxides, and the expense of such separation is significant.

DESCRIPTION OF THE INVENTION

The process for producing 17-oxabicyclo[14.1.0]heptadec-8-ene comprises a reaction in which cyclohexadeca-1,9-diene and hydrogen peroxide are used as reactants.

The molecular relationship of cyclohexadeca-1,9-diene to hydrogen peroxide is, preferably, 1 less than 1, more preferably, 1:0.1-0.9, and, particularly preferably, 1:0.4-0.6.

Cyclohexadeca-1,9-diene and its production are already known, and it is also available commercially. It is often present as a mixture of stereoisomers.

Hydrogen peroxide (H₂O₂) and its production are likewise already known, and it is also available commercially.

A further advantage of the process is that there exists no compelling need to use halogen-containing solvents in the reaction, so that the reaction can be carried out without halogenated solvents—in particular, solvents containing chlorine. In this respect, the need to dispose of the halogenated solvent is eliminated, and there is no danger that undesired halogenated organic compounds will form. Halogen-free solvents such as aliphatic or cyclic hydrocarbons and alkylated aromatics are preferred.

The reaction of cyclohexadeca-1,9-diene and hydrogen peroxide can be carried out in a two-phase system. For example, this can be accomplished by adding to the reactants either no solvent or only very nonpolar solvents (such as toluene) or very polar solvents (such as water).

It is advantageous to use a catalyst in the process, wherein phosphorus-containing or/and tungsten-containing catalysts are especially suitable. Furthermore, the use of a phase transfer catalyst is also advantageous.

The catalyst and its active species are preferably allowed to develop in situ as catalyst precursors. One of the advantages of in situ formation consists in the fact that, unlike ex situ formation, the active species need not be isolated in order to be able to be used in the process. Phosphorus-containing catalyst precursors include, e.g., phosphoric acid, phosphonic acids such as hydroxymethylphosphonic acid and aminomethylphosphonic acid, phosphinic acids such as diphenylphosphinic acid or di(hydroxymethyl)phosphinic acid, and heteropoly acids such as tungstophosphoric acid or molybdophosphoric acid and their derivatives (e.g., lacunar heteropoly acids and polyoxometalates). A variation in the precursor of the phosphorus component is also possible. Therefore, in addition to H₃PO₄, phosphonic acids are very well suited. Hydroxymethylphosphonic acid and phenylphosphonic acid are particularly preferred in this instance.

Tungsten-containing catalyst precursors include, for example, water-soluble tungsten compounds, tungstates, tungsten(VI)-compounds, alkali tungstates, alkaline-earth metal tungstate, ammonium tungstate, or tungsten trioxide monohydrate. Na₂WO₄ is a specific example of a tungsten-containing catalyst precursor.

Examples of a phase transfer catalyst include tetraalkylammonium salt(s) or, preferably, one or more compounds of the formula,

(R¹ _(n)R² _(m)N⁺)_(y)X^(y−),

characterized in that

-   -   R¹ and R² each mean C1-C30 n-alkyl, and R¹ is the same as or         different from R², and the sum of m and n is 4,         X^(y−) equals Cl⁻, Br⁻, I⁻, HSO₄ ⁻, SO₄ ²⁻, H₂PO₄ ⁻, HPO₄ ²⁻,         PO₄ ³⁻, CH₃SO₃ ⁻, CF₃SO₃ ⁻, CH₃C₆H₄SO₃ ⁻, ClO₃ ⁻, ClO₄ ⁻, or NO₃         ⁻, and the sum of m and n equals 4, and y equals 1, 2, or 3.

Preferred anions of the phase transfer catalyst include hydrogen sulfate anions, sulfonic acid anions, or dihydrogen phosphate anions, with hydrogen sulfate anions being particularly preferred.

One example of a phase transfer catalyst is Aliquat 336 ® (trioctylmethylammonium chloride).

It is advantageous if 1 to 3 methyl groups are located on the ammoniacal nitrogen, wherein the remaining alkyl groups on the ammoniacal nitrogen should then have a greater chain length of between 6 and 30 carbon atoms in the chain, with a preferred chain length being between 8 and 22 carbon atoms.

When mixing the tungsten and phosphate-containing catalyst precursors in the presence of hydrogen peroxide and water, peroxotungstophosphates are generated. It is assumed that many suitable peroxotungstophosphates have the {PO₄[WO(O₂)₂]₄}³⁻ anion available.

The cationic component of the active species of the catalyst can be formed from the cation of a phase transfer catalyst; in particular, the cation of the phase transfer catalyst can have the formula,

R¹ _(n)R² _(m)N⁺,

-   -   characterized in that R¹ and R² each mean C1-C30 n-alkyl, and R¹         is the same as or different from R²,     -   and the sum of m and n is 4.

To produce the active species of the catalyst, an aqueous mixture/solution comprising at least one phosphorus-containing acid, at least one tungsten (VI) compound, and at least one phase transfer catalyst and, as the case may be, hydrogen peroxide, can be used. Table A contains examples of the tungsten-containing and phosphorus-containing catalyst precursors and phase transfer catalysts of such aqueous solutions.

TABLE A Tungsten- Phosphorus- containing containing catalyst catalyst Ex. No. precursor precursor Phase transfer catalyst 1 Na₂WO₄ HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 2 Na₂WO₄ HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄  3* Na₂WO₄ HOCH₂P(O)(OH)₂ [CH₃(C₁₈H₃₇)₃N]HSO₄ 4 Na₂WO₄ C₆H₅P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 5 Na₂WO₄ C₆H₅P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄  6* Na₂WO₄ C₆H₅P(O)(OH)₂ [CH₃(C₁₈H₃₇)₃N]HSO₄ 7 Na₂WO₄ H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 8 Na₂WO₄ H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 9 Na₂WO₄ H₃PO₄ [(C₄H₉)₄N]HSO₄ 10  Na₂WO₄ H₃PO₄ [CH₃(C₈H₁₇)₃N]Cl 11  Na₂WO₄ H₃PO₄ [CH₃(C₈H₁₇)₃N]HSO₄ 12* Na₂WO₄ H₃PO₄ [(CH₃)₂(C₁₈H₃₇)₂N]HSO₄ 13* Na₂WO₄ H₃PO₄ [(C₁₈H₃₇)₄N]HSO₄ 14  Na₂WO₄ H₃PO₄ [(CH₃)₃(C₁₆H₃₃)N]O₃SC₆H₄- 4-CH₃ 15* Na₂WO₄ H₃PO₄ [CH₃(C₈H₁₇)₃N]H₂PO₄ 16  Na₂WO₄ (C₆H₅)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄ 17  Na₂WO₄ H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 18  Na₂WO₄ H₃PO₄ [CH₃(C₈H₁₇)₃N]HSO₄ 19  Na₂WO₄ HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 20  Na₂WO₄ (HOCH₂)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄ 21  Na₂WO₄ (HOCH₂)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄

The invention also comprises one or more compounds of the formula,

[R¹ _(n)R² _(m)N+]₃{PO₄[WO(O₂)₂]₄},

-   -   characterized in that     -   R¹ and R² each mean C1-C30 n-alkyl, and R¹ is the same as or         different from R², and the sum of m and n is 4.

These compounds can be used as active species of a catalyst in the inventive process and are generated by the mixing of the already named catalyst precursors and phase transfer catalysts in water in the presence of hydrogen peroxide. Examples of these compounds include

[CH₃(C₈H₁₇)₃N]₃{PO₄[WO(O₂)₂]₄},

[(CH₃)₂(C₈H₁₇)₂N]₃{PO₄[WO(O₂)₂]₄},

[CH₃(C₁₈H₃₇)₃N]₃{PO₄[WO(O₂)₂]₄},

[(C₄H₉)₄N]₃{PO₄[WO(O₂)₂]₄},

[(CH₃)₂(C₁₈H₃₇)₂N]₃{PO₄[WO(O₂)₂]₄},

[(C₁₈H₃₇)₄N]₃{PO₄[WO(O₂)₂]₄}, and

[(CH₃)₃(C₁₆H₃₃)N]₃{PO₄[WO(O₂)₂]₄}.

The inventive process may also comprise a separation step, such as a separation of the phases, distillation, or/and a chromatographic separation.

The process may be conducted discontinuously or continuously.

The following examples clarify the invention, without limiting it in any way.

General Protocol for Examples 1-15 (Table 1)

Na₂WO₄ (0.165 g, 0.50 mmol), H₃PO₄, or one of the listed phosphonic acids (0.50 mmol) and a phase transfer catalyst (0.50 mmol) were placed in a 50 mL three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 25 mmol, 5.51 g), H₂O (5.00 g) and toluene (20.00 g) were subsequently added. Two phases were formed: an organic phase consisting of toluene and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 800 rpm and heated to the reaction temperature of 60° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.47 g, 6.91 mmol, 0.27 mol. equiv.) was added and the reaction started. After 60 min, a second portion of H₂O₂ was dripped in (0.47 g, 6.91 mmol, 0.27 mol. equiv.). Thereafter, it was stirred for another 2 hours at 60° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first two hours and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 1 Phosphorus Conversion Yield Selectivity Examples component Phase transfer catalyst t [min] of CHDD [%] of I [%] to I [%] 1 HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 80 11.4 11.4 100 100 16.3 15.9 97.3 180 30.1 27.7 92.1 2 HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 20 11.8 11.8 100 40 22.1 21.1 95.6 60 22.7 21.7 95.2 80 29.2 27.2 93.2  3* HOCH₂P(O)(OH)₂ [CH₃(C₁₈H₃₇)₃N]HSO₄ 20 12.5 12.5 100 40 21.6 20.1 93.3 60 24.2 22.4 92.5 4 C₆H₅P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 100 14.8 14.8 100 120 19.2 18.3 95.7 180 25.7 23.8 92.7 5 C₆H₅P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 60 19.3 18.5 95.6 80 25.2 23.8 94.5 100 31.6 29.0 91.7  6* C₆H₅P(O)(OH)₂ [CH₃(C₁₈H₃₇)₃N]HSO₄ 60 19.4 18.3 94.3 80 24.3 22.7 93.7 100 31.3 28.8 92.1 7 H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]Cl 60 14.8 14.5 97.9 80 23.3 22.4 96.2 100 32.5 30.2 93.0 8 H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 60 13.2 13.1 99.2 80 23.8 22.5 94.6 100 34.5 31.7 91.8 9 H₃PO₄ [(C₄H₉)₄N]HSO₄ 120 0 0 0 10  H₃PO₄ [CH₃(C₈H₁₇)₃N]Cl 20 15.8 13.2 83.6 60 29.4 25.1 85.4 100 42.1 34.4 81.8 11  H₃PO₄ [CH₃(C₈H₁₇)₃N]HSO₄ 20 10.9 10.7 98.7 40 23.8 22.7 95.3 60 28.7 26.6 92.7 12* H₃PO₄ [(CH₃)₂(C₁₈H₃₇)₂N]HSO₄ 20 10.1 10.1 100 40 20.7 19.4 93.7 80 37.8 34.5 91.4 13* H₃PO₄ [(C₁₈H₃₇)₄N]HSO₄ 60 6.7 6.5 97.2 80 14.4 14.0 97.4 100 23.9 22.6 94.5 120 31.1 28.4 91.2 14  H₃PO₄ [(CH₃)₃(C₁₆H₃₃)N]O₃S—C₆H₄-4-CH₃ 60 12.0 12.0 100 120 24.1 23.0 95.4 180 33.7 31.1 92.1 15* H₃PO₄ [CH₃(C₈H₁₇)₃N]H₂PO₄ 40 18.6 18.1 97.1 60 23.5 22.4 95.3 80 31.1 28.5 91.5 100 37.1 33.8 90.9 *A one-half approach was taken with Example 15 (Table 1), using the following amounts: Na₂WO₄ (0.083 g, 0.25 mmol), H₃PO₄ (0.25 mmol), PTC (0.25 mmol), 1,9-cyclohexadecadiene (2.75 g, 12.5 mmol), toluene (10.0 g), and H₂O (2.5 g), and 2 portions of 50 wt % H₂O₂ (0.24 g, 3.53 mmol, each 0.28 mol. equiv.). The reaction procedure was carried out exactly as described in the general protocol for Examples 1-14.

Protocol for Example 16 (Table 2)

Na₂WO₄ (0.083 g, 0.25 mmol), diphenylphosphinic acid (0.054 g, 0.25 mmol), and methyltrioctylammonium hydrogen sulfate (0.25 mmol) were placed in a 25 mL, three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 12.5 mmol, 2.75 g), H₂O (2.50 g), and toluene (10.00 g) were subsequently added. Two phases were formed: an organic phase consisting of toluene and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 800 rpm and heated to the reaction temperature of 80° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.24 g, 3.53 mmol, 0.28 mol. equiv.) was added and the reaction started. After 60 min, a second portion of H₂O₂ was dripped in (0.24 g, 3.53 mmol, 0.28 mol. equiv.). Thereafter, it was stirred for another 2 hours at 80° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first two hours and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 2 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 16 (C₆H₅)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄ 20 0.2 0.2 99.0 40 2.0 2.0 99.0 60 3.2 3.1 99.0 80 6.2 6.1 99.0 100 11.7 11.3 96.6 120 16.2 15.6 95.9 180 24.1 22.4 93.0 240 28.6 26.0 90.9

Protocol for Example 17 (Table 3)

Na₂WO₄ (0.165 g, 0.50 mmol), aminomethylphosphonic acid (0.50 mmol) and methyltrioctylammonium hydrogen sulfate (0.233 g, 0.50 mmol) were placed in a 50 mL three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 25 mmol, 5.51 g), H₂O (5.00 mL), and 1,2-dichloroethane (20.00 mL) were subsequently added. Two phases were formed: an organic phase consisting of 1,2-dichloroethane and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 700 rpm and heated to the reaction temperature of 60° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (1.10 g, 16.2 mmol, 0.65 mol. equiv.) was added and the reaction started. After 30 min and 60 min, a second portion of H₂O₂ was dripped in (1.10 g, 16.2 mmol, 0.65 mol. equiv. per portion) in each case. Thereafter, it was stirred for another 1.5 hours at 60° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first 100 minutes and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 3 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 17 H₂NCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 20 5.3 5.3 99.0 40 12.4 12.4 99.0 60 25.1 23.5 93.5 80 36.6 33.4 91.3 100 44.9 40.0 89.0

Protocol for Example 18 (Table 4)

H₂WO₄ (0.125 g, 0.50 mmol), phosphoric acid (0.50 mmol) and methyltrioctylammonium hydrogen sulfate (0.233 g, 0.50 mmol) were placed in a 50 mL three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 25 mmol, 5.51 g), H₂O (5.00 mL), and toluene (20.00 mL) were subsequently added. Two phases were formed: an organic phase consisting of toluene and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 700 rpm and heated to the reaction temperature of 60 CC. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.74 g, 10.9 mmol, 0.43 mol. equiv.) was added and the reaction started. After 30 min and 60 min, a second portion of H₂O₂ was dripped in (0.74 g, 10.9 mmol, 0.43 mol. equiv. per portion) in each case. Thereafter, it was stirred for another 1.5 hours at 60 CC. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first 100 minutes and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 4 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 18 H₃PO₄ [CH₃(C₈H₁₇)₃N]HSO₄ 20 24.7 24.7 99.0 40 44.0 41.6 94.5 60 57.2 50.6 88.4

Protocol for Example 19 (Table 5)

Na₂WO₄ (0.165 g, 0.50 mmol), hydroxymethylphosphonic acid (0.50 mmol), and methyltrioctylammonium hydrogen sulfate (0.50 mmol) were placed in a 25 mL, three-necked flask. 1,9-cyclohexadecadiene (mixture of isomers, 25 mmol, 5.51 g) and H₂O (5.00 g) were subsequently added. Two phases were formed: an organic phase consisting of CHDD and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 800 rpm and heated to the reaction temperature of 60° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.47 g, 6.91 mmol, 0.27 mol. equiv.) was added and the reaction started. After 60 min, a second portion of H₂O₂ was dripped in (0.47 g, 6.91 mmol, 0.27 mol. equiv.). Thereafter, it was stirred for another 2 hours at 60° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first two hours and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 5 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 19 HOCH₂P(O)(OH)₂ [CH₃(C₈H₁₇)₃N]HSO₄ 40 13.6 13.6 99.0 100 28.5 27.0 94.9 120 36.5 32.6 89.4

Protocol for Example 20 (Table 6)

Na₂WO₄ (0.083 g, 0.25 mmol), bis(hydroxymethyl)phosphinic acid (0.031 g, 0.25 mmol), and methyltrioctylammonium hydrogen sulfate (0.25 mmol) were placed in a 25 mL, three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 12.5 mmol, 2.75 g), H₂O (2.50 g), and toluene (10.00 g) were subsequently added. Two phases were formed: an organic phase consisting of toluene and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 800 rpm and heated to the reaction temperature of 60° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.24 g, 3.53 mmol, 0.28 mol. equiv.) was added and the reaction started. After 60 min, a second portion of H₂O₂ was dripped in (0.24 g, 3.53 mmol, 0.28 mol. equiv.). Thereafter, it was stirred for another 2 hours at 60° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first two hours and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 6 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 20 (CH₂OH)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄ 20 2.5 2.5 99 40 6.3 6.3 99 60 11.3 11.3 99 80 20.8 20.5 98.6 100 29.2 28.4 97.3 120 32.4 30.7 94.9 180 45.7 40.8 89.3

Protocol for Example 21 (Table 7)

Na₂WO₄ (0.083 g, 0.25 mmol), bis(hydroxymethyl)phosphinic acid (0.031 g, 0.25 mmol), and methyltrioctylammonium hydrogen sulfate (0.25 mmol) were placed in a 25 mL, three-necked flask. 1,9-Cyclohexadecadiene (mixture of isomers, 12.5 mmol, 2.75 g), H₂O (2.50 g), and toluene (10.00 g) were subsequently added. Two phases were formed: an organic phase consisting of toluene and CHDD, and an aqueous phase containing the precursors for the catalyst. The mixture was then stirred at 800 rpm and heated to the reaction temperature of 80° C. Once this temperature was reached, the first portion of H₂O₂ (50 wt %) (0.24 g, 3.53 mmol, 0.28 mol. equiv.) was added and the reaction started. After 60 min, a second portion of H₂O₂ was dripped in (0.24 g, 3.53 mmol, 0.28 mol. equiv.). Thereafter, it was stirred for another 2 hours at 80° C. The progress of the reaction was monitored by taking samples from the organic phase every 20 minutes during the first two hours and at the end of the experiment. The determination of conversion, yields, and selectivities was carried out by means of GC/MS.

TABLE 7 Phosphorus Phase transfer Conversion Yield Selectivity Example component catalyst t [min] of CHDD [%] of I [%] to I [%] 21 (CH₂OH)₂P(O)OH [CH₃(C₈H₁₇)₃N]HSO₄ 20 12.2 12.1 99.0 60 27.1 26.4 97.2 80 39.7 35.2 88.5 100 45.5 39.4 86.5 120 47.4 38.9 82.1 

1. Process for producing 17-oxabicyclo[14.1.0]heptadec-8-ene comprising a reaction with the reactants, cyclohexadeca-1,9-diene and hydrogen peroxide.
 2. Process according to claim 1, characterized in that the reaction is carried out in a two-phase system.
 3. Process according to claim 1 or 2, characterized in that the reaction is carried out in the presence of a catalyst.
 4. Process according to one of the foregoing claims, characterized in that the catalyst contains phosphorus.
 5. Process according to one of the foregoing claims, characterized in that the catalyst contains tungsten.
 6. Process according to one of the foregoing claims, characterized in that the active species of the catalyst contains a peroxotungstophosphate.
 7. Process according to one of the foregoing claims, characterized in that the active species of the catalyst contains the anion, {PO₄[WO(O₂)₂]₄}³⁻.
 8. Process according to one of the foregoing claims, characterized in that the active species of the catalyst contains a cation of a phase transfer catalyst—preferably, a tetraalkylammonium cation.
 9. Process according to one of the foregoing claims, characterized in that the active species of the catalyst contains a cation of a phase transfer catalyst of the formula, R¹ _(n)R² _(m)N⁺, characterized in that R¹ and R² each mean C1-C30 n-alkyl, and R¹ is the same as or different from R², and the sum of m and n is
 4. 10. Process according to one of the foregoing claims, characterized in that the active species of the catalyst is formed from at least one phosphorus-containing acid, at least one tungsten (VI)-compound, and at least one phase transfer catalyst—preferably, in situ.
 11. Process according to claim 10, characterized in that the phosphorus-containing acid is selected from phosphoric acid, phosphonic acids, phosphinic acids, and heteropoly acids and their derivatives, the tungsten (VI)-compound is selected from alkali tungstates, alkaline-earth tungstates, ammonium tungstates, or tungsten trioxide monohydrate—preferably, sodium tungstate—or/and the phase transfer catalyst is selected from a tetraalkylammonium salt—preferably, a compound of the formula, (R¹ _(n)R² _(m)N⁺)_(y)X^(y−), characterized in that R¹ and R² each mean C1-C30 n-alkyl, and R¹ is the same as or different from R², X^(y)-equals Cl⁻, Br⁻, I⁻, HSO₄ ⁻, SO₄ ²⁻, H₂PO₄ ⁻, HPO₄ ²⁻, PO₄ ³⁻, CH₃SO₃ ⁻, CF₃SO₃ ⁻, CH₃C₆H₄SO₃ ⁻, ClO₃ ⁻, ClO₄ ⁻, or NO₃ ⁻, and the sum of m and n equals 4, and y equals 1, 2, or
 3. 12. Aqueous mixture for use as a catalyst precursor in a process according to one of the foregoing claims, comprising at least one phosphorus-containing acid, at least one tungsten (VI)-compound, and at least one phase transfer catalyst.
 13. Compound of the formula, [R¹ _(n)R² _(m)N⁺]₃{PO₄[WO(O₂)₂]₄}, characterized in that R¹ and R² each mean C1-C30 n-alkyl, and R¹ is the same as or different from R², and the sum of m and n is 4, for use as active species of a catalyst in a process according to one of the foregoing claims. 